WO2010015593A2

WO2010015593A2 - Method and device for producing energy, dme (dimethyl ether) and bio-silica using co<sb>2</sb>-neutral biogenic reactive and inert ingredients

Info

Publication number: WO2010015593A2
Application number: PCT/EP2009/060018
Authority: WO
Inventors: Oliver Neumann; Peter Mehrling
Original assignee: Spot Spirit Of Technology Ag
Priority date: 2008-08-07
Filing date: 2009-08-03
Publication date: 2010-02-11
Also published as: WO2010015593A3; US20110135556A1; BRPI0917229A2; DE102008036734A1; CN102112369A

Abstract

Method and devices for producing biosynthesis gases and/or synthetic fuels, in particular DME (dimethyl ether) and/or bio-silica using biogenic ingredients, comprising the steps of: allothermal gasification of the biogenic ingredients by way of pulsed burners for integrated production of process heat in a fluidized bed gasifier; gasification of inert pyrolysis coke from the first gasification step in a second parallel gasification step, which operates according to the principle of an expanded or circulating fluidized bed, using oxygen/steam as the gasification means; combining at least a portion of the gasification product from the two gasifiers for common downstream processing.

Description

Method and device for producing energy, DME

(Dimethyl ether) and bio-silica using CO2-neutral biogenic reactive and inert starting materials

Field of the invention:

On the basis of the gasification processes published by SPOT as patent applications, in the following invention, the SPOT gasification combined process for expanding the spectrum of the biogenic feedstocks to those which, due to their natural consistency, form a reactive pyrolysis coke in the first, simultaneously proceeding step of the gasification reaction (allothermic or autothermic), and the processing of the biosynthesis gas produced in the SPOT gasification process or in the SPOT gasification process into dimethyl ether ( DME) using the modular process routes already described in the application via the isolated intermediate methanol or via the intermediate Forming but not isolated intermediate produced and the preferred use of this product within the INCOX100 process for highly efficient generation of electrical energy.

The gasification process integrates the theoretically and practically available, relevant gasification processes into a new process that, considering the highest standards of economic efficiency, allows all conceivable biogenic feedstocks to be gasified with maximum efficiency (mass conversion rates well above 90%).

The development of thermal gasification processes has essentially produced three different types of gasifier, the entrained flow gasifier, the fixed bed gasifier and the fluidized bed gasifier. In addition, the gasification processes according to the source of Enthalpiestromes required for the gasification reaction m autothermal processes - the reaction enthalpy in the same process by reacting the feedstock to CO2 and H2O (combustion) is produced - or allothermal gasification processes, here is not required for the gasification Enthalpiestrome generated within the process, but spatially separated and supplied to the gasification process by convection, heat transfer (SPOT process) or radiation.

Literature for fluidized bed gasification, which is part of this application, can be found in the following literature: Wolfgang Adlhoch, Rheinbraun AG, Hisaaki Sumitomo Heavy Industries, Ltd., Joachim Wolff, Karsten Radtke (Speaker ), Krupp Uhde GmbH, Gasification Technology Conference, San Francisco, California, USA; October 8 - 11, 2000; Conference Proceedings. Literature for circulating fluidized bed in the composite system, which is a component of this application, can be taken from the following literature: "Decentralized generation of electricity and heat based on biomass gasification", R. Rauch, H. Hofbauer, lecture To Leipzig 2004.

"Circulating fluidized bed, gasification with air, Operation Expenence with CfB Technology for Waste Utilization at a Cement Production Plant", R. Wirthwem, P. Scur, K. -F. Scharf, Rudersdorfer Zement GmbH, H. Hirschfelder - Lurgi Energy and Entsorgungs GmbH; 7th International Conference on Circulation Fluidized Bed Technologies, Niagara Falls May 2002.

The SPOT developments limit the reaction pressure of the gasification process to the low pressure range, because the reaction kinetic characteristics of the gasification process make the space-time yield of the main process apparatus virtually independent of pressure, so that the application of the pressure does not provide the benefit appropriate to the technical requirements of pressure gasification. The reported in the literature multi-stage process, which is essentially (Carbo V, Research Center Karlsruhe) known from the pulverized coal and heavy oil gasification entrained flow gasifier with upstream pyrolysis, appear for technical and economic reasons, completely unsuitable for commercial processes Gasification of biogenic feedstocks.

The fluidized bed gasifiers can be subdivided into two processes: the circulating and the stationary

Fluidized bed gasifier.

In Gussing (Austria), an allothermal, circulating fluidized bed gasification plant was commissioned in early 2002. The biomass is in a fluidized bed with steam as Oxidizing agent gassed. To provide heat for the gasification process, part of the charcoal produced in the fluidized bed is burned in a second fluidized bed. The gasification under steam produces a product gas. Disadvantageous are the high initial costs of the system technology and an excessive effort for the process control.

In order to overcome the problems of the prior art, the Applicant has already filed a number of applications in the field, the disclosure content of which is part of this application. These applications are 10 2006 017 353.8; 10 2006 017 355.4; 10 2006 019 999.5; 10 2006 022 265.2; 10 2006 039 622.7.

From these applications it is known that the biomass is gasified in a fluidized bed with steam as a reaction and fluidizing medium. However, this is a stationary fluidized bed with two specially developed pulse burners, which allow an indirect heat input into the fluidized bed located in the reactor. Hereinafter, this method is referred to as a SPOT method.

Characteristic of the autothermal gasification is the lack of pronounced temperature and reaction zones. The fluidized bed consists of an inert bed material. Thereby, a simultaneous execution of the individual partial reactions and a homogeneous temperature (about 800 ⁰ C) can be ensured. The process is technically feasible, it is characterized by a high efficiency. The acquisition costs are among the aforementioned carburetor types. The SPOT Kombx gasification process

The spectrum has been expanded to include biogenic feedstocks, which tend to form a reaction-bearing coke in the pyrolysis step of gasification. The method is characterized in that the material discharged from the fluidized bed, a mixture of bed material, ash and pyrolysis coke, is fed directly or after screening and screening to separate off the carbon and fines of a second, autothermally operated stationary or expanded or circulating fluidized bed , The product gas, a CO-rich synthesis gas, is added to the main gas stream before gas cooling, the coarse ash is returned to the allothermal gasifier of the SPOT gasification system, and the fine fraction - a high-quality biosilica raw material - is discharged.

The combined product gas from allothermic and autothermal gasification of pyrolysis coke fractions is subjected to dry dedusting, as in the main process, cooled and compressed in order to be fed as compacted biosynthesis gas to the other processes.

method

As a result, it should be noted that via the process routes SPOT gasification by means of SPOT gasification process and / or SPOT combination gasification process a synthesis gas from biogenic feedstocks is available from which in selective synthesis via various process stages m high yield of synthetic fuel DME (dimethyl ether) will be produced; 100 tons of feedstock can be used to produce up to 41 tons of synthetic fuel (DME). The inventive method is based on the above-mentioned patent applications, an allothermal fluidized bed gasification process with special impulse burner for generating the required for the gasification reaction heat, intended for use of gas or so-called off-gases from the further processing of the biosynthetic gas to the final products.

This gasifier is extended by a parallel gasification stage, in which the pyrolysis coke forming during the gasification reaction is converted to synthesis gas by means of steam and oxygen as gasification agent. The entire gasification process is designed as a SPOT combined gasification process in such a way that the proportion of this autothermal gasification stage is minimized, which already requires economic efficiency. The integration of this autothermal sub-process via the ash / Bettmaterialaustrag the allothermal stage and the consideration of the generated synthesis gas for the allothermally produced synthesis gas, so that the further synthesis gas treatment (cooling, etc.) and the treatment of the bed material done together. This autothermal gasifier is an integral part of the SPOT combined gasification process.

With this arrangement, the degrees of conversion of biogenic feedstocks, which form as intermediate gasification (intermediate) inert pyrolysis coke, can be increased to values well above 95%. Due to their silicate content, the resulting ash forms an excellent high-quality bio-silica raw material.

This gasification process involves in situ desulfurization

(Patent Application 10 2007 004 294.0), the hot gas cleaning

(Patent Application 10 2006 017 353.8), the removal of

Halogens by adsorption (Patent Application 10 2007 004 294.0), the use of a single or multi-stage fine cleaning of multicyclone and sintered metal filter, the use of a quencher in which by means of a non-aqueous washing liquid traces of condensable aliphatic and aromatic hydrocarbons are washed out. The separated substances are converted by recirculation in the gasifier to synthesis gas and there is a gas cooling for the subsequent compressor stages.

For the use of biogenic gasification substances which tend to form a reaction coke in the pyrolysis step of the gasification, the cyclically withdrawn from the fluidized bed of the SPOT allothermal gasifier mass flow - a mixture of bed material, ash of the feedstock and pyrolysis coke - directly or after screening and screening for separation of the carbon and in a second gasification step an operating according to the principle of the circulating fluidized bed autothermal gasifier required. This also close atmoshparisch operated gasifier is operated with oxygen / steam as a gasifying agent at temperatures up to about 1000 ⁰ C. Here the pyrolysis coke is reacted. The product gas, a CO-rich synthesis gas, is mixed with the main gas stream before the gas is cooled, and the coarse ash is fed to the allothermal gasifier of the SPOT gasification system. The fine fraction, a high-quality bio-silica raw material, is discharged.

This invention integrates the process routes shown in FIG. 1 for the production of chemicals and synthetic fuels, hydrogen and the generation of electrical or mechanical energy by combustion of the synthesis gas in the gas turbine, boilers, engines or the use z. As the hydrogen in fuel cells, as described in the patent application 10 2007 004 294.0 and the use of synthetic fuel, in particular the DME for the production of electricity in the INCOX100 process.

Overview of the invention:

The present invention relates to the production of the synthetic fuel DME and the generation of electrical / mechanical energy in the context of the INCOXIOO process based on biogenic feedstocks and the biosynthesis gas produced in the SPOT gasification process and the SPOT gasification process also described in the present invention , The present application focuses on the DME fuels with very high yield and economy via the intermediate methanol. A yield of 41 tons per 100 tons of feedstock can be represented. The advantage of this process route over competing processes is simplicity, uniformity, and high yield product availability. In addition to use as a fuel, the use as a liquid gas replacement and as a chemical raw material is possible.

The DME is most suitable for use with INCOX100 (Internal Combustion Box), which is currently available in the two-stroke version up to a mechanical power of 100 MW / h. The application of this technology in the field of power generation, aggregated power up to 1,000 MW / h are possible in a power plant without any problems, and for use for propulsion of ships is obvious. Basically, the DME is also suitable for Four Stroke Combustion Engines. For completeness, the use in gas turbine and boiler is listed. The SPOT combi-gasification process allows the use of an extraordinarily broad spectrum of biogenic feedstocks and extends the applicability of the as part of the invention underlying SPOT gasification process to reaction-inert biogenic feedstocks, which tend to form pyrolysis coke, which is inert in the allothermal gasification step of the SPOT Procedures by the limited here maximum gasification temperature insufficient to convert biosynthesis gas.

The gasification of the entire spectrum of possible biogenic starting materials, including those forming an inert pyrolysis coke for producing the biosynthesis gas and its secondary products, is the object underlying the invention. This object is achieved by a method and a device having the features of the independent claims.

The underlying SPOT gasification process of the allothermal steam gasification with impulse burner is suitable for a wide variety of types of renewable resources, including SPOT's patented Power Greenies, to produce by chemical synthesis for the production of fuels, chemicals and as a feedstock for the production of Energy, combustion in boilers, gas turbines or heat engines with internal combustion suitable to convert ibid described bio-syngas to convert. The applicability of the process is significantly extended by the SPOT combined gasification process developed for the first time.

The SPOT process makes it possible on a large scale to produce energy, fuels and chemical intermediates from renewable raw materials or biomass, which in turn is the starting material for the entire range of products produced today on the basis of petroleum chemistry. The suggested process routes shown in the following description stand so exemplary for the possibilities, but are also the

Key processes that form the interface between renewable resources and other chemical processes based on a closed cycle.

Feedstocks are all renewable raw materials, which - and this is the only theoretical limitation - can be brought to residual moisture content of preferably below 35% mass with an energy cost that is significantly lower than the bound in substance, chemical energy or the corresponding calorific value. Due to the basic reaction conditions, the process is unsuitable for high-aqueous biomass containing only a small percentage by mass of solids (eg Gulle).

The execution of the gasification with two gasification stages allows to use feedstocks which form very inert pyrolysis coke.

By-products and regenerative biomass, power greenies, animal feed, as well as waste from agriculture or food industry, wood of all varieties and species can be extended with this process (the specific adaptations eg of feed preparation and entry into the gasification reactor and bed management are marginal) to convert a circumferentially usable intermediate. Moreover, carrying out the gasification process as an allothermal gasification process in combination with the SPOT combined gasification process makes it extremely efficient to produce a syngas that is otherwise available only by gasification with oxygen. The latter path leads over the technically complex, energetically by the thermodynamic conversion processes low-emission generation of electrical energy and the subsequent production of oxygen. The use of the partial flow gasification, ie the pyrolysis coke which is not sufficiently converted in the allothermal gasifier, does not fundamentally alter this statement.

This conception therefore allows all energies required for production to be CO2-neutral - d. H. to be exported as a net C02 consumer by B. urea synthesis, by which the CO2 content of the synthesis gas is increased and this proportion of CO2 is reacted with produce.

The inventions described below deal with the SPOT combined gasification process and the switching of the process routes, which make it possible to use the biosynthesis gas of the spot gasifier for the production of energy, fuels and chemical products. These routes are characterized by the integrated use of the purge gas (essentially methane) as fuel for generating the heat of reaction of the gasification process in the SPOT gasification process, through energy efficiency and high material utilization of the feedstocks. Part of the invention is the use of the previously described, formed synthetic fuel DME for power generation in the context of the INCOXIOO process.

In detail, the following points are considered:

1. SPOT combined gasification process

2. Use of Off. Purge and other combustible gases generated in the down-stream processes to generate the process heat of the gasification reaction in the pulsed burners of the allothermal SPOT gasification process

3. Mechanical, physical gas purification including gas compression

4. Generation of DME based on biosynthesis gas 5. Generation of mechanical energy (driving power) and electrical energy with DME as feedstock

6. Typical performance data of the INCOXIOO process

7. Generation of electricity by using DME as part of the INCOXIOO process

Production of the following products with biosynthesis gas as a starting point (FIG. 1)

• methanol

• DME via the isolated intermediate methanol or via the intermediate intermediate methanol

• Petrol / diesel via methanol as isolated or intermediate intermediate

• H2 as a feedstock for fuel cells or as a reactant for various chemical syntheses, for example ammonia synthesis and urea synthesis as a secondary product (fertilizer production), olefin syntheses, hydrogenating syntheses, etc.

• Electricity (i.e., mechanical or electrical energy from direct combustion of the biosynthesis gas and use in gas turbines or combustion in the Infernal Combustion Box) also generating mechanical energy and prioritized electric power

• Bio-silica is an environmentally friendly, high-silica raw material derived from the gasification of biogenic agricultural by-products. Due to the high-quality chemical, mineralogical and physical properties, the silicon dioxide (SiO2) extracted from ash is needed as a necessary aid for the production of steel, ceramics, mortar or cement, fertilizer, paper, plastic, cosmetics etc. In the following, the already set forth in the patents, modular process routes are explained again.

The pre-compressed biosynthesis gas is adjusted as part of a clean gas CO shift process with respect to the molar fraction CO / H2 so that the optimum ratio for the further synthesis is achieved.

As a rule, with the exception of H2 production, the CO shift is a partial flow shift. The process integration allows the minimization of the partial flow to be converted in order to achieve the required gas composition.

The synthesis gas adjusted by means of its molar CO / H 2 ratio to the requirements of the subsequent synthesis is then subjected to a gas purification stage for separating the CO 2 content and various trace substances (for example sulfur components) acting as catalyst poisons, as described in the patent application 10 2007 004 294.0 shown gas purification stage shows. This embodiment is exemplary of a number of possible process circuits that fulfill the functionality for reducing the CO2 to a tolerable for subsequent syntheses proportion and removal of trace substances occurring as catalyst poisons. As an alternative to these uses of the synthesis gas, because of the exorbitant high efficiency of INCOX100 according to the Two Stroke or the Four Stroke principle, the use of biosynthesis gas-based synthetic fuel DME and subordinated methanol, diesel or gasoline makes sense.

As a result of the synthesis of methanol and DME, an off-gas, which occurs directly or after separation of hydrogen from this gas mixture z. B. by the pressure swing process directly to Generation of the required for the gasification in the integrated pulse combustors reaction heat can be used.

In Fig. 11, the application is shown as a marine propulsion, here a two-stroke large engine, slow speed, speed range around 100 rpm. For use as a power plant, with a available power of the machine up to 100 MW / h, power plant are up to 1,000 MW / h unproblematic display. With exhaust gas utilization (exhaust gas turbine and exhaust gas utilization with steam turbine), these machines achieve efficiencies well above 70%. In order for this high proportion of mechanical energy to be available for the generator, this combination proves to be the technically superior concept in the field of combined heat and power for the useful portion of low-temperature heat.

Description of the Figures (Figures):

Figures 1a-1c show an overview of the different process routes showing the production of DME and the use of this fuel for use in INCOX100 for power generation and as fuel for gas turbine, boiler and engine in general.

• Fig. 2: two-stage SPOT combined gasification process

• Fig. 3: shows the circuit variant supply of the pulse burner with fuel gas.

• Fig. 4 shows an overview of dedusting, quenching, cooling and compaction.

FIG. 6 shows the overview of the use (or use) of the methanol produced from biosynthesis gas as an intermediate for the production of synthetic aliphatic hydrocarbons, the production of DME (dimethyl ether) as universal fuel and as a precursor for the synthesis of various chemical products.

Fig. 7; DME synthesis from syngas of spot gasification processes

Fig. 8: INCOX100 current in general Fig. 9: INCOX100 specific performance data Fig. 10: INCOX100 application as propulsion of ships Fig. 11: INCOXlOO Excerpt as example Power generation stationary

Detailed description of the embodiments:

The following is a description of the SPOT combination gasification process, the process route for producing the synthetic fuel DME and this use in the context of the INCOXIOO process and gas turbine, boiler, etc. for power generation and / or mechanical (wave) power, as shown in FIG. Ia to Ic are visible.

The present application is an extension of this technology in order to be able to expand the spectrum of starting materials to biogenic starting materials, which tend to form a reaction coke in the pyrolysis step of the gasification. The process is characterized in that the material discharged from the fluidized bed, a mixture of bed material, ash and pyrolysis coke, is fed directly to a second autothermally operated, stationary or expanded or circulating fluidized bed gasifier after screening and sifting to remove the carbon and fines is reacted in which with oxygen and steam as a gasification agent of the pyrolysis coke to synthesis gas. This product gas, a CO-rich synthesis gas, becomes the main gas stream from allothermal gasification before gas cooling added, the coarse fractions of the ashes in the allothermal carburetor of SPOT gasification system returned, the fines - a natural hunger - is discharged. In Fig. 2, the circuit of the two-stage SPOT gasification process is shown.

The following description is exemplary of the arrangement of a second gasification stage in parallel with a SPOT allothermal gasifier. The choice of throughput and throughput ratio between allothermal gasification and autothermal gasification is free and depends on the specific conditions of use, i. H. from the biogenic input materials used. The present invention does not impose restrictions on the flow rate ratio of the two gasification types.

The feedstock Power Greemes is the gasification system preferably m the first stage the allothermal SPOT carburetor with integrated process heat generation impulse burner abandoned (details see the aforementioned SPOT patent applications). The resulting product gas, the biosynthesis gas, is fed after rough dedusting in a gas cooling and a first fine dedusting to get over gas quenching and compression in the down stream processes.

The ash introduced with the feedstock is discharged together with unreacted pyrolysis coke, in the case of feedstocks with formation reaction pyrolysis coke, and sieved and / or sifted in the ash processing so that the carbon-rich (or the entire) fraction is transported to the second gasification stage of the gasification process becomes.

In this stage, which operates on the principle of the expanded or circulating fluidized bed, with oxygen / Steam as gasification medium at temperatures up to 1,500 ⁰ C of the pyrolysis coke to a CO-rich (because of the low H2 content of the feedstock) synthesis gas implemented. It is part of the process of this coke, whose autothermal gasification at higher temperatures is the actual goal of this process stage, the original input materials, where necessary for reasons of gasification processes (mass and heat balance, minimum throughput), mix. This second gasifier is operated with an inert bed, wherein the material must be selected to the gasification temperature significantly higher than the first stage, so under these conditions may not be subject to agglomeration, caking or sticking. The distribution of the gasification agent takes place via the distribution system preserved from the SPOT allothermal stage, the return of the bed material from the expanded fluidized bed takes place via cyclone (high-loaded) with dynamic sealing on the solids side through a barrier section.

The product gas is supplied by way of example to the biosynthesis gas formed in the allothermal gasification and then used as a unit. The separate use is also part of this present invention, but is of secondary interest for practical use.

The use of residual gases (off- or purge gases) of the downstream processes (down-stream processes) as fuel for the pulse burners is described below.

The execution of the SPOT combined gasification process allows the use of the high-calorie off-gases, which are produced as residual gases or purge gases of cycles in the processes described below, as fuel for the impulse burner. System (pulse burner and integrated pilot burner) use. The result of this measure is the increase in the overall efficiency of the process steps and the optimal use of the renewable raw material used. The high calorific off-gas is used to generate the necessary reaction heat of the gasification reactions. The pulse burners and the integrated pilot burners are equipped for this purpose with several independent supply lines for the different fuel gases and exhaust gases. Through this integration of the off-gases, the processes become an integrated element of the SPOT combined gasification process, the process steps to a directly unmistakably connected unit (see Fig. 3 circuit variants, supplying the pulse burner with fuel gas). Another possible variant is the use of these off-gases as fuel gases of the pulse burner, after these z. B. by separation of H2, the reactant z. B. can be used in the synthesis of methanol, were prepared.

The technical equipment allows for starting the normal operation of the gasification plant with bio-synthesis gas, natural gas and propane and the various exhaust gases of the subsequent processes. The concept also allows starting with the help of bio-synthesis gas from the parallel carburettors, even with parallel carburettors. As an extension of the range of use required for starting the carburetor starting materials (fuels of the pulse burner) and the use of the generated from bio-synthesis gas DME (dimethyl ether) is possible and within the meaning of this invention.

The use of a mechanical gas cleaning and fine dedusting by means of multi-cyclone and sintered metal filter (Gaskonditiσnierung before compression of the biosynthesis gas) is provided. It is a compression of the biosynthesis gas and, in consequence of thermodynamic and mechanical requirements, the cooling of the product gas to a temperature range preferably below 100 ⁰ C required. In this temperature range, condensable hydrocarbons present in traces in the biosynthesis gas condense, in particular during startup operation.

The concept described below, the mechanical purification of the biosynthesis gas in the described process stage (FIG. 4) and the cooling in the process stage preferably operated with oil, bio-diesel or other suitable washing and cooling media ensures the required purity and the necessary cooling , The concept avoids the accumulation of technically unusable waste streams. The details of this invention are explained in patent applications 10 2007 004 294.0 and 10 2006 017 353.8.

This is followed by gas compression to the pressure stages necessary for the subsequent processes. The compression of the process stages depends on the requirements of the following processes and becomes necessary when the process pressure of this subsequent process stage is above that of the gasification. This stage can be integrated directly into the process stage or executed separately. In detail, these processes can be described as follows:

• Subsequent processes at the pressure level of the gasification unit: Pressure-free and near-atmospheric processes, such as the combustion of the product gas in boilers or the firing of an industrial furnace (eg rotary kiln for the production of quick lime, cement kiln, etc.) β Follow-up processes with increased pressure

• Processes with integrated compressors (eg turbochargers): As an example, the use of bio-synthesis gas in gas turbines is indicated here. • External compression processes to increase the synthesis gas pressure to the reaction pressure required for subsequent processes. For this purpose, the use in synthesis systems, which are usually operated at a pressure level in the range 20 to 30 bar a.

Another aspect is the production of synthesis gas for power generation (hydrogen), synthetic fuels such as DME and chemical products via direct synthesis or with methanol as an intermediate, as already announced. One of the most important derivatives of biosynthesis gas for use as fuel is DME (dimethyl ether). This product is on the one hand on the isolated methanol methanol synthesis accessible or via the intermediate stage methanol, without its isolation. FIG. 7 shows an overview of the process route of DME production from biosynthesis gas. In addition to the CO conversion, the gas wash, the process routes each include the entire gas generation according to the SPOT process or the SPOT combined gasification process with the purification stages and the compression.

The following description focuses on Figure 7, and in particular on the production of DME (exemplified as a byproduct of the methanol produced in methanol synthesis) and its use as fuel for the application trap for INCOX100 gas turbine and completeness steam boilers.

Other processes, such as the various processes for the production of H2 including its use in fuel cells, the production of ammonia and derived products such as the fertilizer urea, the Fischer-Tropsch process with its variants and secondary products have already been patented filed (patent application 10 2007 004 294.0), so that is waived further explanation.

Essential here is the building on the methanol synthesis, already in the o. G. To emphasize the patent application mentioned synthesis of DME from methanol. This selective, high-turnover process is available in two variants. Once via the isolated (condensed methanol) and directly via the product gas of the methanol synthesis via the gaseous methanol. Both are catalytic processes.

The following description of DME synthesis based on biosynthesis gas follows the illustration in FIG. 7.

The biosynthesis gas is subjected to coarse desulphurisation after the compression stage at a pressure of about 20 bar a to remove traces of sulfur compounds (H 2 S e.a.). The sulfur traces contained in the biosynthesis gas before this process are z. B. absorbed by contact with an iron chelate solution and catalytically oxidized to sulfur, and then for example in a special partial flow CO-shift - processes of a high-temperature CO shift - to be converted. After this conversion, the molar ratio H2 / CO is set, after removal of the main portion of the CO2 content in a chemical washing process and a catalyst pot used to protect the catalyst (zinc oxide catalyst), the conditions for subsequent processes methanol synthesis and the subsequent process the DME synthesis met.

After further compression of the converted, freed of C02 and trace gases synthesis gas, this is the circulation gas stream and from the off (purge) gases of the methanol synthesis z. B. separated by a pressure swing process separated hydrogen and methanol synthesis fed. The crude methanol obtained in this synthesis is subsequently converted into DME in a further process stage.

From the methanol synthesis, the purge gas is separated for equilibration, that is limiting the proportion of non-recyclable components, which is supplied after separation of the hydrogen content of the SPOT gasification process for generating the process heat.

The power generation from biogenic feedstocks, allothermal gasification in the SPOT gasification process and direct combustion of the conditioned gas after gas cleaning, compression and possibly cooling and m the combustor / s of the gas turbine, in the boiler, in directly fired industrial furnace and m internal combustion engines (large engines) was m the patent application 10 2007 004 294.0 described in detail.

With the synthetic fuel DME based on biosynthesis gas, however, is a climate-neutral feed available, by m boiler and gas turbine - such as industrial heat source for decentralized heat production - INCOXIOO process for the production of electric power and as a drive z. As ships, as a fuel in vehicles and as a substitute for liquefied gas available. These applications are listed in Figure Ic.

In the present invention, the use of the product based on the biosynthesis gas is described in the context of the INCOX100 process.

INCOX100 is a process whose core piece is the Internal Combustion Box. This Internal Combustion Box is a combustion unit with internal combustion, integrated combustion control and exhaust expansion. This device is available with two- and four-stroke operation up to Outputs of 100 MW / h el. available. In both cases, the energy of the flue gas stream of combustion after internal expansion by exhaust gas turbine and by Abwarrnenutzung, steam generation and use in steam turbine and optionally used by means of thermal power coupling for generating mechanical energy and / or electricity. Application of this technology in the field of power generation leads without problems by the technically available module capacity of 100 MW / h to possible power generation plants (INCOX100-power plants) of 1,000 MW / h and more.

Another essential aspect of the INCOXIOO process is the charging of the combustion air to achieve optimum efficiency of the engine, the achievement of a high, technically achievable internal pressure, which occurs during combustion at the beginning of the power stroke, the use of the energy of the flue gases after combustion by exhaust gas turbine (Expansion turbine, which once compresses the combustion air and uses the rest of the expansion work to drive a generator), and beyond the enthalpy of the combustion gases / flue gases) to use for steam generation.

In addition, the extraction of heat for heating purposes (heat and power coupling) is provided. This process achieves mechanical efficiencies well over 70% with the described exhaust gas utilization. With integrated heat and power coupling, this efficiency can be increased, at least theoretically, by more than 15 efficiency points. This inventive concept with heat and power coupling is characterized by the high mechanical efficiency (thus indicating the very high electrical efficiency), which is a factor of two above the current power plants. It is the technical top concept in the field of combined heat and power, as the useful temperature / heat for heating purposes is lower, but does not have to be permanently removed.

Claims

claims

1. A process for the production of biosynthesis gases and / or synthetic fuel, in particular DME (dimethyl ether) and / or bio-silica, using biogenic starting materials, comprising the steps:

- Allothermal gasification of the biogenic feedstock using pulse burners for the integrated generation of process heat in a fluidized bed gasifier;

- Gasification of reaction pyrolysis pyrolysis from the first gasification stage in a second, gasification stage, which preferably operates in parallel, which operates on the principle of expanded or circulating fluidized bed, by means of oxygen / steam as a gasification agent

- bringing together at least part of the gasification products from the two carburetors for joint further processing.

2. The method according to the preceding claim, wherein the discharged material is subjected to a screening and / or screening for the separation of the carbon and / or the fines for the isolation of the m ash contained in the bio-silicate.

3. The method according to one or more of the preceding claims, wherein the coarse fractions of the ashes are recycled to the allothermal gasifier and / or the Fexnanteil of the ash is discharged as a high quality biosilicate product.

4. The method according to one or more of the preceding claims, wherein the further processing of the biosynthesis gases comprises one or more of the following steps:

- In-situ desulfurization

- Hot gas cleaning

- Removal of halogens by adsorption

- Single or multi-stage fine cleaning with multicyclone and sintered metal filter

- Using a quench, are washed out by means of a non-aqueous washing liquid traces of condensable aliphatic and / or aromatic hydrocarbons

- Gas cooling for the subsequent compressor stages

5. The method according to one or more of the preceding claims, wherein from the generated biosynthesis gas via the intermediate stage methanol dimethyl ether (DME) is produced.

6. The method according to one or more of the preceding claims, wherein the reaction-pyrolysis coke formed in the allothermal gasification (based on the biogenic feedstock) is reacted in a second gasification stage with an oxygen / vapor mixture as a gasifying agent.

7. The method according to one or more of the preceding claims, wherein pre-compressed biosynthesis gas in the context of a pure gas CO-shift process with respect to the molar fraction CO / H2 is adjusted so that optimal conditions are achieved for the further synthesis.

8. Apparatus for the production of biosynthesis gases and / or synthetic fuel, in particular DME (dimethyiether), using biogenic starting materials, comprising the components: - Allothermal fluidized bed gasifier for the gasification of the biogenic feedstock by means of pulse burners for the integrated generation of process heat;

- Another carburetor, which is preferably arranged in parallel, according to the principle of the expanded or circulating fluidized bed as a second gasifier for the gasification of reaction-pyrolysis coke from the first gasification stage by means of oxygen / steam as a medium

- Means for bringing together at least a part of the gasification products from the two carburetors for the common further processing

9. The apparatus of the preceding apparatus claim, wherein there are means for subjecting the discharged material to screening and / or sifting to separate the carbon and / or feme portions to isolate the bio-silicate contained in the ash.

10. The device according to one or more of the preceding device claims, wherein means are provided which return the coarse fractions of the ashes to the allothermal gasifier and / or which discharge the fines of the ash as a high quality biosilicate product.

11. The device according to one or more of the preceding device claims, wherein the further processing of the biosynthesis gases is carried out by one or more of the following means:

- In-situ desulphurisation agent

- means for hot gas cleaning

- means for the removal of halogens by adsorption

- Means for single or multi-stage fine cleaning with multicyclone and sintered metal filter - Quenching, are washed out by means of a non-aqueous Waschflussigkeit traces of condensable aliphatic and / or aromatic hydrocarbons.

- means for gas cooling for the subsequent compressor stages

12. The device according to one or more of the preceding device claims, wherein means are present which produce from the biosynthesis gas generated via the intermediate methanol Dirnethylether (DME).

13. The apparatus according to one or more of the preceding device claims, wherein the reaction-inert pyrolysis coke formed in the allothermal gasifiers is reacted in a second gasification stage with carburetors operating on the principle of the expanding or circulating fluidized bed by means of oxygen / steam as the gasification agent.

14. The device according to one or more of the preceding device claims, wherein means are present, the precompressed biosynthesis gas in the context of a clean gas CO shift process with respect to the molar fraction CO / H2 adjusted so that the optimum ratio for the further synthesis is achieved ,

15. Use of a device according to one or more of the preceding device claims for the production of fuel for a two-stroke engine or four-stroke engine, in particular on a ship.

16. The use according to the preceding claim, characterized in that DME or synthesis gas for, preferably an INCOX100 (Internal Combustion Box) is used for power generation in a two-stroke version.

17. The use according to the preceding claim, characterized in that the ash obtained on the basis of synthesis gas production is used to produce bio-silica.